CN1051902A - Catalyst regeneration process in the synthesizing ethyl benzene method - Google Patents
Catalyst regeneration process in the synthesizing ethyl benzene method Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
A kind of catalyst regeneration process that is used for gaseous ethene-benzene catalytic alkylation system benzene process.Present method has comprised using can pursue the multistage reactor simulation moving-bed system that bed switches; Catalyst regeneration can be realized the mitigation regeneration condition of normal pressure, permanent oxygen amount, can realize that flexible is switched, the recovery time.Thereby, can significantly improve the efficient of catalyzer, prevent temperature runaway, guard catalyst, energy efficient, easy and simple to handle, flexible.
Description
The present invention relates to the method for catalyst regeneration in the alkylated reaction, furtherly, relate to and use the AF-5 molecular sieve; The method for preparing the reprocessing cycle use of the AF-5 molecular sieve in the benzene process by gaseous ethene-benzene catalytic alkylation.
Be used for the catalyzer that ethene and benzene prepare the method for ethylbenzene, that know is Al Cl
3, but select Al Cl for use
3As catalyzer, just produced more serious burn into pollution problem in the reaction process inevitably.Be detrimentally affect all to be arranged, and the aftertreatment more complicated need processing such as alkali cleaning, washing, causes problems such as the three wastes once more to production unit or to producing environment.
Disclose in the United States Patent (USP) 4136128 with containing Z SM-35, the Si-Al zeolite of Z SM-38 is made the technology of Preparation of Catalyst ethylbenzene.Disclose in the United States Patent (USP) 4169111 with containing weight less than 0.7%() Na
2The acid Si-Al zeolite of O is made the Preparation of catalysts benzene process.Japanese Patent J61126041 discloses with the method that prepare ethylbenzene of aluminium-silicate crystal in the presence of hydrogen.
U.S. Mobil company discloses the method for gaseous ethene-benzene Si-Al zeolite as Preparation of Catalyst ethylbenzene in its United States Patent (USP) 3751504,3751506 and 4107224, and eight two groups the exchange reaction-regeneration system that is adopted.
In prior art, also have, such as disclosed catalyzer in the Chinese patent application numbers 87105054, many to power in the method for improving catalyzer and catalyst regeneration.If can effectively utilize catalyzer, improve catalyst efficiency, prolong catalyzer work-ing life, at the industrial cost that can reduce the preparation benzene process significantly.But in above-mentioned technology, the method for preparing ethylbenzene is to adopt the method for fixed bed substantially.For example, eight two groups of Mobil exchange reaction-regeneration systems also promptly become one group with four reactor secure bond, and when a group reaction, another group is carried out behind the catalyst regeneration stand-by.Each bank of reactor is a fixed bed basically in entire reaction period.In order to prolong reaction time, must set up active gradient at bed, make the final stage bed have the usefulness of deposit layer, for this reason, must adopt the higher catalyst bed of L/D value, its consequence is that whole reactor group pressure reduction increases, and has increased the compression energy consumption; In order to prolong reaction time, avoid too high by product production rate simultaneously, also must improve the extent of dilution of temperature of reaction and reaction gas, this has just increased heat energy consumption, thinner circulating consumption and product separation energy consumption; In order to prolong reaction time, if need delay the inactivation process, can only under high reaction pressure, could better realize, increased the compression energy consumption equally.
Under above-mentioned reaction conditions, the catalyst regneration difficulty needs to adopt conventional more harsh regeneration condition, and this has just increased unreliability and insecurity.
The purpose of this invention is to provide a kind of raising catalyst efficiency, catalyzer can be under the mitigation condition regenerated, stable operation, the catalyst regeneration process that is used for gaseous ethene-benzene catalytic alkylation system benzene process that the method continuity is good.
The purpose of this invention is to provide a kind of catalyst regeneration process that is used for gaseous ethene-benzene catalytic alkylation system benzene process, make reaction still can stablize, incessantly, and can highly transform and less energy-consumption ground safe operation at handoff procedure.
The objective of the invention is to finish based on following design.
Set up a simulation moving-bed multistage reactor, each reactor is connected mutually and is formed the system that is communicated with, wherein each reactor can be one by one switches to come out to carry out after the catalyst regeneration process as terminal section back into system successively from system, simultaneously, the remaining reaction device in the system still link to form connected system mutually and reacts.Described multistage reactor, it comprises 3 above reactors, is 4 to 7 reactors preferably, be 5 reactors best, each reactor is a fixed bed, is connected by the good valve of sealed against leakage performance and pipeline etc. between the reactor, forms placed in-line coherent system.Each reactor is pressed
(catalyst primary first-order equation cycle)/(reactor number)
Average time interval, from system, switch one by one and regenerate, the system that cuts again after the regeneration goes round and begins again as the end reaction bed, carries out stable, continual continuity operation.
Fig. 1 is a simulation moving-bed synoptic diagram of the present invention.
Fig. 2 is that regenerated inactivation form synoptic diagram (supposing the four stars phase of running period) is switched in five series connection of the present invention.
Fig. 3 is for burning carbon TG curve.
The burning carbon TG curve of 0.2%-1.0% oxygen level when Fig. 4 is 480 ℃.
Fig. 5 burns carbon speed graph of a relation for oxygen level.
Each reactor of the present invention can be an adiabatic reactor.
In simulation moving-bed multistage reactor of the present invention, can switch and more than one reactor as the catalyst regeneration bed, be to switch a reactor preferably as the catalyst regeneration bed.
Gaseous ethene-benzene catalytic alkylation system ethylbenzene of the present invention can have long-term operation and short period running.
As shown in Figure 2, suppose that switching time, T in T(figure referred to a week), so, each reaction bed catalyzer participates in the time (also promptly with time of reaction mass actual contact) of reaction, be respectively from the 1st to the 4th 3T, 2T, T(wherein 4T be catalyst (always) reaction times once).Because the catalyzer of end reaction section is fresh all the time and keep high reactivity, so even initial reaction section activity drops to below 90%, the transformation efficiency that ethene, benzene prepare ethylbenzene can remain on more than 99% equally.Thereby, can obviously prolong the catalyst primary first-order equation cycle.Same reason, the simulation moving-bed low pressure drop bed pattern that adopts of the present invention reduces system pressure drop greatly.
Similarly, because the level of deactivation of final bed is decided by the switching interval time
((total reaction time of catalyst)/(reaction bed))
To delay the inactivation process be secondary cause thereby make, and for this reason, gaseous ethene of the present invention-benzene catalytic alkylation reaction can carry out under lower pressure.Similarly, the temperature of reaction of gaseous ethene of the present invention-benzene catalytic alkylation reaction does not need very high yet.
Gaseous ethene of the present invention-benzene catalytic alkylation prepares benzene process and can select for use the AF-5 molecular sieve as catalyzer, and its particle diameter can be a φ 1-3 millimeter, length 2-6 millimeter.After catalyzer is because of reason inactivations such as cokings, make its regeneration by the burning decoking.Catalyst regeneration condition of the present invention can be a demulcent.
Catalyst regeneration choose opportunities of the present invention conversion of ethylene in reactor is reduced to below the 90%-98%, is preferably, at 90%-95%, preferably below 95%.At this moment, this section reactor is switched from system as the original segment reactor, also, it is stopped into ethene and benzene, and feed nitrogen.
Catalyst regeneration can carry out under normal pressure in gaseous ethene of the present invention-benzene catalytic alkylation method, and common pressurized conditions for purposes of the invention not necessarily.Can select to carry out under the pressure of 1 kg/cm to 3 kg/cm the manipulation of regeneration of catalyzer.Equally, the common requirement that needs to increase oxygen-adding amount in catalyzer burns the regeneration process of carbon neither be necessary to the present invention.It can be to carry out under permanent oxygen amount that catalyzer of the present invention burns the carbon processing, and common oxygen level is less than 1.2%, is preferably less than 1.0%.
Catalyzer of the present invention burns charcoal regeneration to be handled and can carry out under 330 ℃ to 600 ℃ temperature, is the scope at 450 ℃ to 520 ℃ preferably, also is, when need that section of regenerated reactor from system, switch come out after, feed nitrogen, heating is warming up to above-mentioned scope gradually.Temperature is too low, and it is just long to burn the carbon required time, and processing is also incomplete, temperature is too high, has accelerated although burn carbon, and the destructible catalyzer also easily causes fluctuation of service, such as temperature runaway, waits detrimentally affect.
Time of burning the C catalyst manipulation of regeneration of the present invention is not particularly limited, is generally more than 4 hours, and be 8 to 48 hours preferably, look the coking degree, burn the carbon temperature and decide, the recovery time can also be controlled at consistent with switching cycle.
That section reactor of handling by catalyst regeneration process method of the present invention switched when regenerating in next time, entered reaction system with regard to the terminal section reactor of conduct and reacted (as shown in Figure 2), and at this moment, the catalyzer in this section reactor is highly active.
It is of the present invention that to be used for the advantage that gaseous ethene-benzene catalytic alkylation prepares the catalyst regeneration process of benzene process be tangible, the regeneration handoff procedure of catalyzer is steady flexibly, can rationally regulate switching cycle to adapt to various rigor condition, improve the catalyzer service efficiency.It is little single switching time influence to be fallen in pressure one by one, and system fluctuation is little, and is just smaller to follow-up continuity method influence.
Of the present invention thereby to be used for another advantage that gaseous ethene-benzene catalytic alkylation prepares the catalyst regeneration process of benzene process be can adopt regenerative process time and the corresponding to short period operation of switching interval to remain the high reactivity of catalyst and thereby can carry out high yield production with the catalyst filling amount of minimum.Shorten reaction time thus, can further reduce the generation of harmful side product.And few because of coking, inactivation is little, regeneration condition more relaxes.
Of the present invention to be used for another advantage that gaseous ethene-benzene catalytic alkylation prepares the catalyst regeneration process of benzene process be that the catalyst regeneration condition relaxes, and practicable normal pressure, permanent oxygen level, homothermic burn the carbon method.To preventing temperature runaway, protection catalyst activity and assurance safety have significant superiority.
Further specify the gaseous ethene-benzene catalyst alkylation that is used for of the present invention below in conjunction with embodiment and prepare the catalyst regeneration process of benzene process.
In following embodiment, the ethene of selecting for use is technical grade, and ethylene content is that 95-99%, ethane content are that 0.3-1.2%, methane and hydrogen richness are 0.7-4.3%, is provided by the Shanghai Gaoqiao petroleum chemical plant; Benzene is technical grade, is provided by factory of shanghai refinery and Shanghai Coke Plant;
Embodiment 1
Reaction process synoptic diagram shown in Figure 1 and reactor in be packed into 312.5 kilograms of solid AF-5 molecular sieves respectively.After the static draining of benzene, through the benzene evaporator evaporation, and cross the thermosetting benzene vapour, again through transferpump, enter I section reactor by pipeline 2.Ethene is sent into surge tank under 5 kg/cm pressure, through constant voltage, with weight space velocity (kilogram ethene/kilogram catalyzer hour) 1.0 hours
-1Send into I section reactor, II section reactor by pipeline 3.4.5 and 6 respectively, III section reactor and IV section reactor.The inlet temperature of each section reactor is 380 ℃, and working pressure (gauge pressure) is 5 kg/cm.Sending into the benzene of I section reactor and the mol ratio of ethene is 14: 1.The discharging of I section reactor is sent into II section reactor by pipeline 7, the discharging of II section reactor is sent into III section reactor by pipeline 8, the discharging of III section reactor is sent into IV section reactor by pipeline 9, and the discharging of IV section reactor is sent into follow-up distillation process by pipeline 10.The results are shown in table 1.
When the conversion of ethylene that records initial reaction section (here corresponding be I section reactor) is lower than 95%, I section reactor is switched, also be about to pipeline 3 and close, pipeline 7 and II section reactor are thrown off, and pipeline 2 is received II section reactor.Simultaneously, the V section reactor that carried out catalyst regeneration process is connected on after the IV section reactor, sends to follow-up rectifying with the discharging of V section reactor.I section reactor is burnt the C catalyst manipulation of regeneration, is that the experimental result of the II, III, IV of original segment reactor and the reaction system that V section reactor is formed is with table 5 with II section reactor.
Feed nitrogen to from reactive system, switching the II section reactor that has stopped into ethene and benzene that comes out, under normal pressure, feed mixed gas (nitrogen+air), the oxygen level of this mixed gas heats up gradually less than 1.0%, constant temperature is 30 minutes to about 420 ℃ the time, and about 8 hours of combustion time, the promotion to 500 of bed temperature is to 510 ℃, by gas-chromatography, the content that records carbonic acid gas is zero.
Through burning the I section reactor of C catalyst manipulation of regeneration, when switching next time, enter next reactive system as the terminal section reactor of above-mentioned V section reactor conduct.Circulation so repeatedly.
Embodiment 2
Five catalyst regeneration process that switch in the regeneration system benzene process to carrying out as embodiment 1 have also carried out catalyst stability and have burnt the carbon characteristic test.
The catalyst stability experiment comprises the specific surface area before and after the catalyst regeneration, intensity, measurements such as X ray diffracting spectrum.Strength trial shows that the average intensity before the catalyst regeneration is 4.5 kilograms/, and the average intensity after the regeneration is 4.6 kilograms/, changes being no more than 3%.Chromatography is surveyed the specific surface area test and is shown preceding average out to 345 meters squared per gram of catalyst regeneration, and the average specific surface area after the regeneration is 345, no change.X-ray diffracting spectrum shows, and is consistent before and after the catalyst regeneration.
The TG curve of burning carbon shows that weightlessness mainly occurs in 400 ℃ to 520 ℃ as shown in Figure 3.Burn the burning carbon TG test that the carbon characteristic test also comprises 480 ℃ of temperature, 0.2%, 0.4%, 1.0% oxygen level.As shown in Figure 4.The carbon that burns under the different oxygen under the differing temps is tested, and obtains as shown in Figure 5 oxygen level and burning carbon speed graph of a relation.
As mentioned above, the catalyst regeneration process that gaseous ethene-benzene alkylation of the present invention prepares in the benzene process can be realized normal pressure, and permanent oxygen amount etc. relax regeneration condition, can realize the flexible switching recovery time.Be contemplated that with the present invention variation all should be considered to belong to scope of the present invention on basic any regeneration condition, and not only be limited to the above embodiments.
Claims (10)
1, a kind of method that is used for the catalyst regeneration of gaseous ethene-benzene catalytic alkylation system benzene process is characterized in that described alkylation reaction method has comprised that use multistage reactor switches regeneration system rapidly; Described catalyst regeneration process comprises Regenerative beds is stopped into ethene and benzene, feeds nitrogen under 1 kg/cm to 3 kg/cm pressure, feeds the mixed gas of constant oxygen level, heats up gradually to burn at 330 ℃ to 600 ℃ to burn carbon and handle.
2, by the described method of claim 1, it is characterized in that described catalyzer is a solid AF-5 molecular sieve.
3, by the described method of claim 1, it is characterized in that described mixed gas is nitrogen and Air mixing gas, oxygen level is between 0.2% to 1.2%.
4, by the described method of claim 3, the oxygen level that it is characterized in that described mixed gas is 0.2% to 1.0%.
5, by the described method of claim 1, the temperature that it is characterized in that burning carbon is 420 ℃ to 550 ℃.
6, by the described method of claim 5, the temperature that it is characterized in that burning carbon is 480 ℃ to 510 ℃.
7, by the described method of claim 1, it is characterized in that catalyst regeneration carries out under normal pressure.
8, by the described method of claim 1, it is characterized in that described multistage reactor switches regeneration system rapidly and comprises the series system that 3 above reactors are connected, wherein each reactor can be one by one switches to come out to carry out behind the catalyst regeneration as terminal section reactor back into reactive system successively from system, simultaneously, the remaining reaction device in the system still link to form connected system mutually and reacts.
9,, it is characterized in that described multistage reactor switches regeneration system rapidly and is made of 5 adiabatic reactors by the described method of claim 8.
10, by claim 1,8,9 described methods, it is characterized in that from described switching regeneration system rapidly, switching a reactor as the catalyst regeneration bed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89106037A CN1051902A (en) | 1989-11-11 | 1989-11-11 | Catalyst regeneration process in the synthesizing ethyl benzene method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89106037A CN1051902A (en) | 1989-11-11 | 1989-11-11 | Catalyst regeneration process in the synthesizing ethyl benzene method |
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| CN1051902A true CN1051902A (en) | 1991-06-05 |
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| CN89106037A Pending CN1051902A (en) | 1989-11-11 | 1989-11-11 | Catalyst regeneration process in the synthesizing ethyl benzene method |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503760A (en) * | 2011-10-11 | 2012-06-20 | 中国石油化工股份有限公司 | Device and method for prolonging regenerate cycle of alkylation catalyst in ethylbenzene process |
| CN102875320A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Aromatics methylation tandem reaction method |
| CN102875321A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Method for continuous production of p-xylene through aromatic hydrocarbon alkylation |
| CN111569954A (en) * | 2020-04-30 | 2020-08-25 | 常州瑞华化工工程技术股份有限公司 | Method for removing liquid-phase benzene retained in catalyst of liquid-phase ethylbenzene alkylation and transalkylation reactor by superheated benzene vapor purging |
| CN112876381A (en) * | 2021-04-14 | 2021-06-01 | 江苏扬农化工集团有限公司 | Simulated moving bed device and method for preparing 6-aminocapronitrile by gas phase method |
-
1989
- 1989-11-11 CN CN89106037A patent/CN1051902A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102875320A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Aromatics methylation tandem reaction method |
| CN102875321A (en) * | 2011-07-12 | 2013-01-16 | 中国石油化工股份有限公司 | Method for continuous production of p-xylene through aromatic hydrocarbon alkylation |
| CN102875320B (en) * | 2011-07-12 | 2015-01-07 | 中国石油化工股份有限公司 | Aromatics methylation tandem reaction method |
| CN102875321B (en) * | 2011-07-12 | 2015-01-07 | 中国石油化工股份有限公司 | Method for continuous production of p-xylene through aromatic hydrocarbon alkylation |
| CN102503760A (en) * | 2011-10-11 | 2012-06-20 | 中国石油化工股份有限公司 | Device and method for prolonging regenerate cycle of alkylation catalyst in ethylbenzene process |
| CN111569954A (en) * | 2020-04-30 | 2020-08-25 | 常州瑞华化工工程技术股份有限公司 | Method for removing liquid-phase benzene retained in catalyst of liquid-phase ethylbenzene alkylation and transalkylation reactor by superheated benzene vapor purging |
| CN112876381A (en) * | 2021-04-14 | 2021-06-01 | 江苏扬农化工集团有限公司 | Simulated moving bed device and method for preparing 6-aminocapronitrile by gas phase method |
| CN112876381B (en) * | 2021-04-14 | 2024-01-26 | 江苏扬农化工集团有限公司 | Simulated moving bed device and method for preparing 6-aminocapronitrile by gas phase method |
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